Process for the selective oxidation of hydrocarbons

ABSTRACT

The invention relates to a heterogeneous vanadium-phosphorus oxide catalyst system for the selective oxidation of hydrocarbons, which may or may not be saturated, comprising a support based on one or more metal oxides, and vanadium-phosphorus oxide in an amount of from 0.01 to 45 wt. %, based on the weight of the catalyst and calculated as (VO) 2  P 2  O 7 , to a process for the selective oxidation of an organic compound in the presence of a vanadium-phosphorus oxide catalyst, which process comprises an oxidation and a reduction phase, wherein a hydrocarbon is contacted with said catalyst in the reduction phase and in oxidized or non-oxidized form is adsorbed to the catalyst, whereafter the thus loaded catalyst is brought into the oxidation phase, the desired product is formed in the presence of gaseous oxygen and subsequently separated.

This application is a division of application Ser. No. 08/234,657, filedApr. 28, 1994 now U.S. Pat. No. 5,707,917.

FIELD AND BACKGROUND OF THE INVENTION

This invention relates to a catalyst for the selective oxidation ofhydrocarbons, which may or may not be saturated, to oxygen-containingorganic compounds. More particularly, the invention relates to acatalyst for the selective oxidation of hydrocarbons tooxygen-containing compounds, such as the oxidation of n-butane to maleicacid anhydride. The invention further relates to a process for theselective oxidation of hydrocarbons, which may or may not be saturated,to oxygen-containing organic compounds. Finally, the invention alsorelates to the preparation of such a catalyst.

According to the prior art, n-butane is oxidized to maleic acidanhydride with a good selectivity in the presence of catalystscontaining vanadium oxide and phosphate. Suitable catalysts can beprepared in two different manners. In both cases, the starting materialis vanadium(V), whereafter the vanadium(V) is reduced to vanadium(IV),whereafter phosphate is added. According to the first method,hydrochloric acid is added to the solution of vanadium(V), whereafter atelevated temperature the vanadium is reduced with hydrogen chloride toform chlorine. According to the second method, work is done in anorganic solvent, such as for instance i-butanol. At elevated temperaturethe organic solvent reduces the dissolved vanadium(V) which issubsequently stabilized by reaction with the dissolved phosphate.

In general the selective oxidation is carried out with an excess ofoxygen. To prevent the formation of explosive mixtures, generally acontent of 1.5 vol. % n-butane in air is worked with. Typical is aconversion of about 90% of the n-butane present in the feed, which isconverted to maleic acid anhydride with a selectivity of about 60%. Torealize such a conversion, the temperature of the catalyst bed must bemaintained at about 400° C. Naturally, with such an exothermic reactionthe temperature in the catalyst bed will increase; generally, a higherfinal temperature leads to a poorer selectivity with a higherconversion. About 50% of the n-butane supplied then becomes available asmaleic acid anhydride with the current technical implementation of theprocess.

Customarily, the oxidation reaction over the vanadium, phosphorus andoxygen-containing catalysts is carried out by passing the reactantsthrough the reactor once, a so-called `once through` process. One of themost important limitations of this process, which uses a fixed catalystbed, is that only an n-butane concentration of 2 vol. % at most can beused; higher n-butane contents may lead to explosions.

To increase the yield of maleic acid anhydride, recently otherembodiments of the process have been proposed. One of the successfulnewly proposed embodiments is a fluidized bed reactor. It is thenpossible, without danger of explosions, to increase the concentration ofthe n-butane in the feed to substantially the stoichiometric value. As aresult, the productivity per unit volume of the reactor increases, whichleads to lower investment costs. (GB-A 2,145,010).

A fluidized bed reactor has still other advantages, viz. a markedlyimproved dissipation of the reaction heat, so that areas having locallya high temperature are effectively avoided. Although a fluidized bedprocess is economically and technically attractive, the selectivity ofthe catalytic oxidation is lower at higher n-butane concentrations,while moreover a (highly) wear-resistant catalyst must be used. Inparticular in the case of vanadium-phosphate-oxygen catalysts, theproduction of a wear-resistant catalyst is a difficult task.

It is known from EP-A 189,621 that the efficiency of the conversion tomaleic acid anhydride can be increased by employing two separatereaction steps. The two reaction steps are carried out in separatereactors or in separate sections of a single reactor. In this case,n-butane, preferably in the absence of molecular oxygen, is contactedwith the oxidized catalyst. After reaction with the lattice-oxygenpresent in the catalyst, whereby maleic acid anhydride is formed with agood selectivity, the residual butane and the product formed areremoved, and the catalyst is passed into a reoxidation zone, where thecatalyst is reoxidized with air oxygen.

Since the reduction and the oxidation of the catalyst take place inseparate reactors, a more concentrated n-butane stream can be used.Moreover, in such a circulating fluidized bed, the heat transferproceeds faster than in a fixed catalyst bed, so that the temperature isbetter controllable. Selectivity of up to 90% has been reported for theuse of this process with two separate catalytic reactors. Although theyield of maleic acid anhydride is markedly increased, the catalystdeveloped for this process has two shortcomings. Because theconventional vanadium-phosphorus-oxygen catalyst is not wear-resistant,a new catalyst had to be developed, whose individual catalyst bodies arecovered with a porous layer of silicon dioxide. On the one hand, thisporous layer reduces wear, but, on the other hand, the inert porouslayer limits the transport of reactants and reaction products. Moreover,the surface/volume ratio of the vanadium-phosphorus-oxygen constituentin the newly developed catalyst is relatively low, as in theconventional catalysts. To obtain a useful conversion of n-butane, largequantities of catalyst have to be recirculated per kilogram of maleicacid anhydride. In the literature it has been published that perkilogram of catalyst only about 2 g maleic acid anhydride is obtained.

It appears from the above-described prior art that there is a great needfor a better catalyst in order to overcome the drawbacks of the currentvanadium-phosphorus-oxygen. In general, wear-resistant catalysts inwhich the catalytically active component has a high surface area tovolume ratio are obtained by providing the active component on aso-called support. Such a support is a highly porous, thermostablematerial, on the surface of which the active component or components areprovided in more or less finely divided form. Commercially, a widevariety of preformed support bodies are available; it is therefore easyto select a suitable support with the necessary wear-resistance and adesired pore distribution. If the active component or components areprovided on a support selected on the basis of the process in which thecatalyst is to function, a catalyst meeting often conflictingrequirements is readily obtained.

In spite of the fact that the vanadium-phosphorus-oxygen has alreadybeen employed on a technical scale for over a decade and in spite of thefact that the shortcomings of the current catalyst have been suitablyrecognized, efforts to prepare a satisfactory supportedvanadium-phosphorus-oxygen catalyst have been unsuccessful to date. Theselectivity of the supported vanadium-phosphorus-oxygen catalystsprepared heretofore was invariably found to be unacceptably low.

This is the reason that alternatives have been searched for. The firstpossibility has already been mentioned above, viz. the provision of aporous layer of wear-resistant silicon dioxide on porous particles ofthe vanadium-phosphorus-oxygen catalyst. Another method of preparing animproved catalyst is described in the above-mentioned GB-A 2,145,010.There a mixture of the oxides of vanadium and phosphorus is treated withan acid, preferably phosphoric acid or hydrochloric acid, the materialthus obtained is mixed with zirconium dioxide or titanium dioxide, andthe suspension obtained is subsequently spray-dried. Wear-resistantbodies of dimensions of from 3 to 10 μm are then obtained. It will beclear that neither of the methods leads to catalysts where the activecomponent is provided on (highly) porous support bodies in finelydivided form.

An important disadvantage of the known catalysts based on vanadium,phosphorus and oxygen (VPO) is, moreover, the requirement that thecatalysts must possess a specific structure to obtain the desiredactivity and selectivity.

A first object of the present invention is to provide a suitablecatalyst for the selective oxidation of hydrocarbons, which catalyst isless dependent on the structure of the active component and whichmoreover requires no special measures for increasing its usefulness invarious more modern oxidation processes.

SUMMARY OF THE INVENTION

Surprisingly, it has now been found that the provision of (hydrated)vanadium(III) oxide on a suitable support, either simultaneously withphosphate or followed by reaction of the hydrated vanadium(III) oxideprovided on the support with phosphate leads to catalysts which exhibitexcellent properties for the oxidation of hydrocarbons. It is known thaton non-alkaline support materials, such as silicon dioxide, hydratedvanadium(III) oxide can be provided in extremely finely divided form,preferably by deposition-precipitation. On aluminum oxide and titaniumdioxide, too, vanadium(III) oxide can in this way be applied asextremely small particles with a homogeneous distribution over thesurface of the support. Surprisingly, in the reaction with phosphates orwith phosphoric acid a catalyst is formed which yields an eminentactivity and selectivity.

The invention primarily relates to a heterogeneous vanadium-phosphorusoxide catalyst system for the selective oxidation of hydrocarbons, whichmay or may not be saturated, comprising a support based on one or moremetal oxides, and vanadium-phosphorus oxide in an amount of from 0.01 to45 wt. %, based on the weight of the catalyst and calculated as (VO)₂ P₂O₇.

It has been found that such a catalyst on support, where the amount ofsupport is at least 55 wt. % and more particularly more than 60 wt. %,and where the VPO component has been applied to the surface of thesupport, can be readily used in a variety of selective oxidationprocesses, exhibits hardly any wear, if at all, and requires no specificstructure of the VPO component. More particularly, it has been foundthat no limitations with regard to transport arise in the catalystsystem.

BREIF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a graph of carbon concentration versus time useful inexplaining the invention;

FIG. 2 is a further graph of carbon concentration versus time useful inexplaining the invention; and

FIG. 3 is yet a further graph of carbon concentration versus time usefulin explaining the invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT

According to a preferred embodiment of the invention, the VPO componentis well dispersed over the surface of the support.

With the catalysts according to the invention, it is of importance thatthe surface of the support is occupied with the finely divided activecomponent or components as uniformly as possible. The best way ofdetermining the occupation of the surface of a support with activecomponent is X-ray photoelectron spectroscopy (XPS). With this techniquethe chemical composition of the surface layer of the catalysts can bedetermined. The ratio of the intensities of a type of atoms forming partof the support and of vanadium is representative of the extent to whichthe surface of the support is covered with active component. If we takea titanium oxide support as an example, then the ratio of theintensities of titanium and vanadium in the X-ray photoelectron spectrumof the catalyst is a measure for the occupation of the support surfacewith the active component. In the case of a high ratio, the surface ispoorly covered by the vanadium, whilst in the case of a lower ratio, thesurface of the titanium dioxide support is homogeneously occupied withsmall particles. Naturally, the load of the support also plays a role.In the case of a low load of the support, a high ratio in the X-rayphotoelectron spectrum will be measured sooner than in the case of ahigh load.

It has been now been found that the product of the ratio of theintensities of a type of atom of the support and vanadium in the X-rayphotoelectron spectrum and the load expressed in the load in percent byweight is a good indication of the extent of dispersal. In practice thismeans that the dispersion number, the measure for the dispersal, has avalue between 0.01 and 500, more particularly between 0.01 and 300. Thedispersion number is defined as the product of the percentage by weightof VPO, calculated as (VO)₂ P₂ O₇ on the catalyst, and the atomic ratioof metal of the support component, in this connection understood toinclude silicon, to vanadium determined with XPS. XPS is described interalia in the article of Brinen et al, X-Ray Photoelectron spectroscopystudies of the rhodium on charcoal catalyst, J. of Catalysis, 40,295-300 (1975), using a correction for the background according toShirley, D. A. Shirley, Phys.Rev.B, 1972, 5, 4709.

Because the amount of support in the catalyst is of great significance,catalysts according to the invention contain an amount of supportmaterial constituting a minimum of 55% and preferably a maximum of 95%of the weight. The use of a suitable support is of importance becausethe support is generally cheaper than the vanadium. In addition, thewear-resistance of the catalyst is higher in the case of a high supportmaterial content. Other advantages of providing the active component(s)on a suitable support are the fact that the specific surface and thepore distribution of the support can be selected, so that impediments totransport can be prevented. In addition, it has been found,surprisingly, that if particular support materials, such as titaniumdioxide, are used, the catalytic properties of the active component aremodified. The extent to which the catalytic properties are affecteddepends on the load; a lower load leads to a stronger effect of thesupport on the catalytic properties. In this way, the catalyticproperties of the catalyst can be controlled as well.

The catalyst according to the invention preferably contains, as support,one or more metal oxides, in this connection understood to include, bypreference, titanium oxide, zirconium oxide, silicon dioxide, aluminumoxide or combinations thereof. The content of support is preferably atleast 75 wt. %, since such a content already yields good results.

An important advantage of the catalyst according to the invention isthat it is already active at lower temperatures. With the presentcatalyst, temperatures lower than 360° C. suffice.

The invention also relates to a process for the selective oxidation ofhydrocarbons, using such a catalyst. More particularly, the inventionfurther relates to a process for the selective oxidation of hydrocarbonsof the above-described type, where the catalyst is passed throughoxidation and reduction zones, in which process the present catalyst canbe suitably used.

It has now been found that the above-mentioned process in which thecatalyst is recirculated from a zone where the catalyst reacts with theorganic compound to a zone where the catalyst is reoxidized, can beconsiderably improved. In accordance with the improved process, thecatalyst is also recirculated between an oxidation and a reduction zone,but the catalyst, before it is passed into the reoxidation zone, isallowed to remain loaded with adsorbed, partially oxidized saturatedhydrocarbon, whereafter the thus adsorbed hydrocarbon, after transfer,is allowed to react in the second reaction zone with gaseous oxygen orwith other compounds to form oxygen-containing products.

The invention accordingly relates to a process for the selectiveoxidation of an organic compound in the presence of avanadium-phosphorus oxide catalyst, which process comprises an oxidationand a reduction phase, wherein a hydrocarbon is contacted with saidcatalyst in the reduction phase and in oxidized or non-oxidized form isadsorbed to the catalyst, whereafter the thus loaded catalyst is broughtinto the oxidation phase, the desired product is formed in the presenceof gaseous oxygen and is subsequently separated.

According to the invention it is possible to use a fixed catalyst bedand to pass alternately (air) oxygen and a saturated hydrocarbon throughthis bed. Selective oxidations which can be carried out in accordancewith the present invention are the oxidation of C₄ hydrocarbons to formthe various oxidized variants thereof, such as butene, butadiene,crotonic aldehyde, 2,5-dihydrofuran, maleic acid, tetrahydrofuran andmaleic acid anhydride. Oxidation of pentane yields inter alia phthalicacid anhydride. Preferably, the process according to the invention iscarried out with n-butane, the reaction product being maleic acidanhydride.

To enable the partial oxidation of the saturated hydrocarbon or then-butane to adsorbed reactive species, the saturated hydrocarbon or then-butane should preferably be contacted with the catalyst at arelatively low temperature. At such a low temperature, which ispreferably between 200 and 500° C., then only a very minor amount ofbutane per unit weight of the catalyst reacts. It is observed that inthis connection it is possible to work the reduction phase and theoxidation phase at different temperatures.

When using the catalyst according to the present invention, atemperature of less than 360° C. can be employed in the reduction phase,whilst the oxidation phase can be worked at temperatures below 300° C.

In general, the process according to the invention can be carried out ina number of ways. In the first place, it is possible to work thereduction phase in the absence of oxygen or in the presence of a minorproportion of oxygen with regard to the hydrocarbon. The oxidation phasecan be carried out in the absence of hydrocarbon or in the presence ofan amount of hydrocarbon which is present in a minor proportion withregard to the amount of oxygen. This can be realized by appropriatelyfeeding oxygen and hydrocarbon to the reactor or reactors. An importantvariant of the process according to the invention is formed by thesupply of a relative minor proportion of hydrocarbon to the oxidationzone. In this way a considerable increase of the yield of oxidationproduct is obtained. Apart from the yield of the oxidation of thehydrocarbon in the reduction zone using the oxygen bound to thecatalyst, a second product stream is obtained in this way. As a mirrorimage of this variant, a minor proportion of oxygen can be fed to thereduction zone. Thus, already in the reduction zone the desiredoxidation product is formed, which can be removed from the reductionzone.

In the practice of the process according to the invention, thehydrocarbon can be supplied in undiluted form, but it is also possibleto dilute it with an inert gas. Non-absorbed hydrocarbon, if any, isremoved from the reduction zone and recirculated after treatment, ifany. Preferably used as oxidizing component is molecular oxygen, eitherin the form of air or in more purified form. Although this is notpreferred, it is also possible to use other oxidizing components, whichhave an effect comparable to oxygen.

It is noted that in the practice of the process according to theinvention at least a part of hydrocarbon is transported from thereduction zone to the oxidation zone in adsorbed, partially oxidizedform, which is clearly different from the known processes. The fact is,in these processes a separation of the hydrocarbon occurs at the end ofthe reduction zone. In accordance with the invention, the catalyst has aconsiderable load with hydrocarbon. In general, this load is at least0.05 wt. % based on the weight of the catalyst.

Because of its good selectivity, the process according to the inventioncan be used with conventional catalysts, for instance as described inU.S. Pat. Nos. 4,371,702 and 4,632,916. In accordance with a preferredembodiment of the invention, the use of the above-described catalystwith a high surface area/volume ratio of the active phase on a supportis highly attractive.

Such a catalyst can be obtained by providing the vanadium component witha valence of from 2.5 to 4.5 on the support, more particularly byhomogeneously increasing the pH of a suspension of a suitable support ina solution of a vanadium salt in which the vanadium has an adjustableaverage valence which may vary between 2.5 and 4.5, and phosphate. Thishomogeneous adjustment of the pH can be effected in a number of ways. Afirst possibility is the injection of a compound such as urea under thesurface of the well-stirred suspension. Another method is described inapplicant's European patent application 225,659, by which method theactive component is precipitated on the support in an electrochemicalcell using an electrical current to be passed through the cell.

It is also possible to apply the vanadium component by impregnation ofthe support with a solution of a suitable vanadium salt, for instancevanadyl(IV)acetyl acetonate, whether or not in the presence of aphosphate component.

The preparation of the vanadium solution of lower valence preferablyoccurs by an electrochemical reduction of vanadium(V) in accordance withthe prior art, as described in European patent application 223,299.

However, it is also possible to prepare the vanadium of lower valence indifferent ways in accordance with the current state of the art.Surprisingly, it has been found that in this way finely divided vanadiumoxide/phosphate can be provided on supports such as titanium dioxide,zirconium oxide, aluminum oxide and silicon dioxide.

The phosphorus-oxygen component is preferably applied prior to, duringor after the application of vanadium component. The application ispreferably effected by means of a compound based on a phosphorus oxide,for instance one or more phosphates and/or a phosphorus-based acid.

Examples of suitable compounds are alkali metal and ammonium phosphates.

The catalyst obtained after calcination of the loaded support is highlywear-resistant and has a high active surface per unit weight. By virtueof this high specific surface of the active phase, the reaction with thesaturated hydrocarbon can be carried out at temperatures as low as 300°C. or less while yet a high conversion per unit weight of catalyst isobtained. Accordingly, the process according to the invention willpreferably be carried out with the above-described catalyst.

It is of great importance to control the transport of oxygen and thesaturated organic compound in the catalyst bodies as well as possible.When a fixed catalyst bed is used, a catalyst with wide pores isrequired, since the allowable pressure drop across the catalyst beddisenables the use of small catalyst bodies (for instance less than 0.5mm). Given the relatively large, minimum pore length in the catalystbodies to be used, the pore diameter must be chosen to be relativelylarge. In a fluidized bed much smaller catalyst bodies, for instance of100 μm, can be used. As a consequence, in fluidized bed catalystsnarrower pores can be used. In accordance with the process according tothe invention, the catalyst support can be selected such that, forspecified dimensions of the catalyst bodies, the associated optimum porediameter is obtained. With the current state of the art this is notpossible with VPO catalysts.

Suitable supports preferably have a surface area between 1 and 400 m²/g, determined by the BET method. Examples of suitable commerciallyavailable supports are:

a) Titanium dioxide, Engelhard 0602P, BET surface 100 m² /g

b) Titanium dioxide of Degussa (P25) having a surface of 50 m² per gram.The titania support was also modified with a temperature treatmentwhereby the surface and the pore distribution were varied.

c) Silicon dioxide of Degussa (OX 50) having a surface of 50 m² per gram

d) Zirconium oxide, Daiichi 132-1, BET surface 40 m² /g

e) Aluminum oxide of Degussa (C100) having a surface of 100 m² per gram,which may or may not have been priorly saturated with phosphate, inorder to prevent absorption of the phosphate component by the supportmaterial during the preparation proper.

f) Silicon dioxide of Degussa (P 200) having a surface of 200 m² pergram.

The invention will now be further explained in and by a few examples,which should not be regarded as limitative.

EXAMPLES 1 AND 2

In accordance with the principle of the deposition precipitation fromhomogeneous solution on suspended supports, a few catalysts wereprepared.

Vanadium(V) was electrochemically reduced in acid solutions of a pH<2 tovanadium having an initial valence of 3.7 on average. The phosphate tovanadium ratio was adjusted to 1.1:1 with a phosphate donor, forinstance NH₄ H₂ PO₄. In a suspension of Degussa P25 (titanium dioxidewith a surface of 50 m² per gram, which had been modified by atemperature treatment whereby the surface and the pore distribution weremodified) the pH was homogeneously increased with exclusion of oxidizingcomponents, such as oxygen from the air, by injecting a 1% solution ofammonia. The pH of the solution was 1.9 at the start and 7.0 at the end.Thus a titanium oxide-supported VPO catalyst with a load of 8.8 percentby weight, based on (VO)₂ P₂ O₇, was obtained. The dispersion number ofthe catalyst was 51.9. After testing, this number was determined again,which resulted in a value of 44.

The catalyst was tested, i.e. first the catalyst was loaded with butane(10% butane in argon, space velocity 2000 per hour) for 5 minutes in afixed bed with 1.5 ml catalyst of a weight of 1.43 g (catalyst sievefraction 0.09-0.15 mm) and subsequently, in a separate step, afterflushing with argon at a space velocity of 4000 per hour, it wasreoxidized for 2 minutes with a varying amount of oxygen (20 to 2%oxygen in argon, space velocity 2000 per hour). It can be seen in FIG. 1that the selectivity to the desired product, being maleic acidanhydride, varies at the maximum amount of product stream between 40 and50% for oxygen concentrations varying from 20 to 2%. The yield ofproducts decreases with decreasing oxygen concentration, but theselectivity increases. The concentration of maleic acid anhydride (=54;maleic acid anhydride contains 4 C atoms, which means that theconcentration of maleic acid anhydride corresponds with the carbonconcentration/4) decreases with decreasing oxygen concentrations, butthe concentrations of CO (=28) and CO₂ (=44) decrease more. Thetemperature at which the above-mentioned butane adsorption step wascarried out was 273° C. The temperature at which the oxidation can becarried out and at which the loading can be carried out can, inprinciple, be adjusted independently when the gas streams are separated.However, this is not so easy with a fixed bed as described above. It wasalso found that the temperature rose (at least to 281° C.) in thereoxidation with oxygen. The amount of butane which was presented peramount of catalyst on the surface and was oxidized off it upon 20% O₂for 2 minutes was 0.5 g/kg catalyst in the case of this catalyst underthe above-mentioned conditions (10% butane for 5 minutes, at atemperature of 273° C.). The concentrations at which the catalyst bedwas passed through continuously were 1.5% butane and 20% oxygen in argonat a space velocity of 2000 per hour. These are the flat portionsbetween the peaks as shown in FIG. 1. The production increase upon theoxygen pulse after loading with butane can be clearly seen. Further,experiments have demonstrated that even when the catalyst is loadedagain, a reasonable amount of maleic acid anhydride is produced. Thisamount represents a selectivity of 30% at a minimum and 60% at amaximum.

A catalyst was prepared with an initial valence of vanadium of 2.9 onaverage and an adjusted phosphate to vanadium ratio of 1.1:1, supportedon Degussa P25 with a load of 8.8 percent by weight, based on (VO)₂ P₂O₇. The pH of the solution was 2.0 at the start and 7.0 at the end. ThepH was increased by injecting a 1% solution of ammonia. The catalyst hada dispersion number of 52.8. The catalyst was tested, i.e. first thecatalyst was loaded with butane (respectively, 20 and 10% butane inargon, space velocity 2500 per hour) for 5 minutes in a fixed bed with1.2 ml catalyst of a weight of 1.2 g (catalyst sieve fraction 0.09-0.15mm) and subsequently, in a separate step, after flushing with argon at aspace velocity of 5000 per hour, it was reoxidized for 2 minutes with avarying amount of oxygen (20 to 4% oxygen in argon, space velocity 2500per hour). It can be seen in FIGS. 2 and 3 that the selectivity to thedesired product, being maleic acid anhydride, varies at the maximumamount of product stream between 33 and 40% for oxygen concentrationsvarying from 20 to 2%. The yield of products decreases with decreasingoxygen concentration, but the selectivity increases. The concentrationof maleic acid anhydride (=54, maleic acid anhydride contains 4 C atoms,which means that the concentration of maleic acid anhydride correspondswith the carbon concentration/4) decreases with the decreasing oxygenconcentrations, but the concentrations of CO (=28) and CO₂ (=44)decrease more. The total production of products in the case of loadingwith 20% butane is higher than in the case of 10% butane. However, theselectivity to the desired product, maleic acid anhydride, is slightlylower. The temperature at which the above-mentioned steps were carriedout was 298° C. The concentrations at which the catalyst bed wascontinuously flown through were 1.5% butane and 20% oxygen in argon at aspace velocity of 2500 per hour. These are the flat parts between thepeaks shown in FIGS. 2 and 3. The production increase upon the oxygenpulse after loading with butane can be clearly seen. It was also foundthat the temperature rose (at least to 310° C.) in the reoxidation withoxygen. After testing, the catalyst had a dispersion number of 48.4.

As will appear clearly from the above-mentioned examples, the amount ofbutane which can be activated at the surface depends on the temperatureat which the adsorption occurs and on the butane partial pressure towhich the catalyst is exposed. The amount which can be oxidized off itagain depends on the temperature at which the reoxidation occurs and atwhat oxygen partial pressure this occurs.

We claim:
 1. A preparative process for the selective oxidation of anorganic compound in the presence of a vanadium-phosphorus oxidecatalyst, which process comprises a reduction phase and an oxidationphase, said preparative process comprising the steps of:employing afixed bed or a fluidized bed reactor, said reactor comprising avanadium-phosphorus oxide catalyst; passing through said reactor a feedstream comprising a hydrocarbon, wherein said hydrocarbon is contactedwith said catalyst in the reduction phase of said process and inpartially oxidized or non-oxidized form is adsorbed to the catalyst toform a loaded catalyst; passing through said reactor anoxygen-containing gas, wherein the loaded catalyst is brought into theoxidation phase of said process and the desired product is formed in thepresence of gaseous oxygen; continuing to pass alternately through saidreactor said feed stream comprising said hydrocarbon and saidoxygen-containing gas; and isolating said desired product following eachoxidation phase.
 2. A process according to claim 1, wherein a fixed bedof vanadium-phosphorus oxide catalyst particles is used and alternatelyan oxygen-containing gas and a feed stream with hydrocarbon are passedthrough the bed.
 3. A process according to claim 1, wherein maleic acidanhydride is prepared by oxidation of n-butane.
 4. A process accordingto claim 1, wherein a catalyst on support is used, based on a metaloxide support.
 5. A process according to claim 4 wherein the metal oxidesupport is selected from the group consisting of titanium oxide,zirconium oxide, silicon dioxide, aluminum oxide and combinations of twoor more of these oxides.
 6. A process according to claim 1, wherein anamount of hydrocarbon is supplied to the oxidation phase, in a minorproportion with regard to the amount of oxygen.
 7. A process accordingto claim 1, wherein an amount of oxygen is supplied to the reductionphase, in a minor proportion with regard to the amount of hydrocarbon.8. The process according to claim 1, wherein said catalyst is aheterogeneous vanadium-phosphorus oxide catalyst system comprising asupport based on one or more metal oxides, said support having asurface, and vanadium-phosphorus oxide in an amount of from 0.01 to 45wt. %, based on the weight of the catalyst and calculated as (VO)₂ P₂O₇, wherein said vanadium-phosphorous oxide component is well-dispersedover said surface of said support, and wherein said catalyst has adispersion number between 0.01 and 500, said catalyst having been madeby a process that includes a step of applying the vanadium containingcomponent to the surface of the catalyst support by homogeneouslyincreasing the pH of a suspension of a suitable support in a solution ofvanadium salt, in which the vanadium has an adjustable average valencewhich may vary between 2.5 and 4.5, phosphate being present before,during or after said step.
 9. The process according to claim 8, wherein,in said catalyst system, said support is selected from the groupconsisting of titanium oxide, zirconium oxide, silicon dioxide, aluminumoxide and combinations of two or more of these oxides.
 10. The processaccording to claim 8, wherein, in said catalyst system, said catalysthas been made by a process further including the steps of drying andcalcining, to form a supported vanadium-phosphorus oxide catalyst. 11.The process of claim 8, wherein, in said catalyst system, said catalysthas a dispersion number between 0.01 and 300.